CN1014118B - Catalytic reactor - Google Patents
Catalytic reactorInfo
- Publication number
- CN1014118B CN1014118B CN88102903.3A CN88102903A CN1014118B CN 1014118 B CN1014118 B CN 1014118B CN 88102903 A CN88102903 A CN 88102903A CN 1014118 B CN1014118 B CN 1014118B
- Authority
- CN
- China
- Prior art keywords
- catalyst bed
- interchanger
- catalyticreactor
- reaction vessel
- radially
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 7
- 239000003054 catalyst Substances 0.000 claims abstract description 79
- 239000007789 gas Substances 0.000 claims description 36
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 239000000376 reactant Substances 0.000 claims description 16
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 3
- 239000011949 solid catalyst Substances 0.000 claims description 3
- 239000007795 chemical reaction product Substances 0.000 claims description 2
- 238000012423 maintenance Methods 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 239000012495 reaction gas Substances 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000000112 cooling gas Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005553 drilling Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000002459 sustained effect Effects 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- IXSZQYVWNJNRAL-UHFFFAOYSA-N etoxazole Chemical compound CCOC1=CC(C(C)(C)C)=CC=C1C1N=C(C=2C(=CC=CC=2F)F)OC1 IXSZQYVWNJNRAL-UHFFFAOYSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0403—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
- B01J8/0407—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
- B01J8/0415—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being superimposed one above the other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00194—Tubes
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A catalytic reactor includes a reactor vessel, a catalyst bed and at least two heat exchangers. The catalyst bed and heat exchangers are arranged coaxially with the central axis of a reactor vessel and substantially at the same height.
Description
The invention relates to a kind of being used for, and gas raw material is contacted with the solid catalyst of catalyst bed, the heat release conversion reaction takes place, thus, obtain the catalyticreactor of gaseous reaction product gas raw material importing catalyst bed.
Usually, in catalyticreactor, a catalyst bed is divided into several less catalyst beds, and between per two continuous less catalyst beds, insert interchanger, its result, the temperature in each less catalyst bed can maintain in the scope that is suitable for most carrying out of desired reaction, thus, make the reaction of being carried out reach best degree.Up to the present, in known vertical catalyticreactor, all be that this less catalyst bed is set one by one individually, each catalyst bed wherein is made of the inside and outside cylinder that gas can pass through, and their top and bottom are all sealed.The cross section of each catalyst bed all is an annular, and profile is cylindric, allows reactant gases radially to flow through, and therefore, the pressure of gas during by catalyst bed just falls and can reduce.
In the catalyticreactor of prior art, following catalyticreactor is disclosed recently.
Day disclosure special permission communique 81-81129
Day disclosure special permission communique 85-110328; 85-179131,
In these disclosed catalyticreactors, the position of interchanger all is located at, for example, and annular catalyst open central space, or the top of the catalyst bed in reaction vessel or lower space.
In above-mentioned prior art, catalyst bed and interchanger only are arranged in the space of reaction vessel, yet do not consider maintenance and working cost problem fully.In addition, they also have some following shortcomings:
1. catalyticreactor internal structure complexity, and manufacturing expense height.
2. the interchanger of assembly and disassembly catalyticreactor is time-consuming and bother.After having only catalyzer to draw off fully, just might take out interchanger, therefore, the maintenance of catalyticreactor is difficult to carry out, and causes repair expense higher.
3. interchanger is according to the thermal design that produces in the corresponding catalyst bed, owing to provide the space of mounting heat exchanger limited, therefore, the size of the interchanger of designing like this is difficult to coupling with corresponding catalyst bed.
Purpose of the present invention is exactly in order to have overcome the shortcoming of above-mentioned catalyticreactor, and to provide a kind of be the catalyticreactor of feature with easy maintenance and low manufacturing expense.
In catalyticreactor of the present invention, be provided with a catalyst bed and at least two interchanger with the vertical central shaft of reaction vessel is coaxial, and they are located substantially on same vertical height.It is the position that several baroque interchanger are installed in easy checking maintenance together.For example: at the topmost of catalyticreactor, thereby the maintenance interchanger is convenient, and simultaneously, needed maintenance cost has also reduced.
Fig. 1 is the longitudinal diagram that the present invention has been used for an embodiment of reactors for synthesis of ammonia.
Fig. 2 is the partial longitudinal section of an alternative embodiment of the invention, has wherein revised the design of second interchanger 8 among Fig. 1.
Fig. 3 is the longitudinal diagram of another embodiment that is used for the reactor of synthetic ammonia, wherein is provided with two interchanger, an outside that is arranged on catalyst bed, and another is arranged on the inside of same catalyst bed.
Fig. 4 is the longitudinal diagram that is used for another embodiment of reactors for synthesis of ammonia, and wherein two interchanger all are arranged on the outside of a catalyst bed.
Above-mentioned several embodiment of the present invention will be described in detail with reference to accompanying drawing hereinafter.
At first referring to Fig. 1, this catalyticreactor comprises reaction vessel 1, three catalyst bed bodies in this reaction vessel 1, i.e. first catalyst bed 4, second catalyst bed 5 and the 3rd catalyst bed 6, they one be arranged on below another, and first interchanger 7 and second interchanger 8 all are arranged in the center drilling of first catalyst bed, 4 inside.
First other the pipe 10 and second other pipe 11 is set, imports cooling gas from the outside, so that be controlled at the temperature of the reactant gases of each position in the reaction vessel 1.Yet, because cooling gas do not mix with reactant gases, therefore, the reactant gases gas dilution that can not be cooled.
In many reactive systems, all use tubular heat exchanger as interchanger.In addition, the parts of an interchanger, for example, housing and tube sheet usually are used as the parts of another interchanger or corresponding catalyst bed.In illustrated embodiment, the inner housing 7A of first interchanger also is used as the body skin of second interchanger 8, and the body skin 17 of first interchanger 7 separates first interchanger 7 also as a dividing plate from first catalyst bed, 4 residing spaces.
Inner side-wall near reaction vessel 1 is provided with first and second inner cylinders 2,3, therein, above-mentioned catalyst bed 4,5,6 and interchanger 7,8 has been installed.First and second inner cylinders 2,3 are as the stationary member of these intrawares 4,5,6,7 and 8, simultaneously also as the hot plate washer of reaction vessel 1.Formed space all is used as the passage of air-flow between the narrow space that is limited between the reaction vessel 1 and first inner cylinder 2 and first and second inner cylinder 2,3.
The flow direction and the influence of gas will be described hereinafter.
Unreacted live gas, enter catalyticreactor by gas inlet 14, upwards flow in space between the reaction vessel 1 and first inner cylinder 2, enter the upper end of the shell-side of second interchanger 8, carry out heat exchange with the reactant gases of discharging from second catalyst bed 5, then, flow out by the lower end of second interchanger 8.In addition, fresh gas enters in the tubulation of this interchanger by the lower end of first interchanger 7, carries out heat exchange with the reactant gases of discharging from first catalyst bed 4, and is heated to the initial temperature of catalyzed reaction by this, then, flows out through the upper end of interchanger 7.Heated like this live gas, the outer cylindrical wall by first catalyst bed 4 enters first catalyst bed 4, when live gas radially inwardly flows through catalyst bed 4, just carries out catalyzed reaction.Then, the reactant gases of generation enters the shell-side of this interchanger in the upper end of first interchanger 7, here is cooled, and flows out through the lower end of this interchanger.Then, the reactant gases that is cooled like this enters this catalyst bed 5 by the outer cylindrical wall of second catalyst bed 5, and at this, reactant gases further carries out catalyzed reaction.The reactant gases that generates flows out by the inner cylinder wall of second catalyst bed 5, and enters the tubulation of second interchanger 8, and here because the result of the heat transferred live gas of reactant gases, itself is cooled reactant gases.After this, reaction gas flow is by pipe 12, then by the space between first inner cylinder 2 and second inner cylinder 3, in the 3rd catalyst bed 6, carry out last catalyzed reaction after, flow out catalyticreactors by pneumatic outlet 15.
The embodiment of Fig. 2, except the design of second interchanger 8 had been revised, all the embodiment with Fig. 1 was identical basically for other.
In the embodiment that Fig. 2 describes, respectively the gas of shell-side by second interchanger 8 and tubulation be among the embodiment with Fig. 1 antithesis, that is to say, fresh gas flow is the upper end that enters the tubulation 16 of second interchanger 8, and second catalytic bed, 5 effusive reaction gas flows are gone forward side by side into the lower end of the shell-side of second interchanger 8 to the upper reaches.After the reaction gas of catalyst bed 5 and live gas carry out heat exchange, reaction gas from the upper end of shell-side downwards stream by central row tracheae 13 then, by the cylinder inner wall inflow catalyst bed 6 of the 3rd catalyst bed 6.
Above-mentioned structure does not need second inner cylinder 3, thus, makes the structure of catalyticreactor obtain simplifying.
Referring to Fig. 3, first interchanger 7 is arranged on the outside of first catalyst bed 4 below, and second interchanger 8 is arranged on the inside of first catalyst bed 4.Shown in orthographic plan, first and second interchanger 7,8 and the 4 coaxial settings of first catalyst bed, therefore, the vertical central shaft of they and reaction vessel 1 is coaxial, and is located substantially on sustained height.
In the embodiment shown in fig. 4, first interchanger 7 is arranged on the outside of first catalyst bed 4, and second interchanger 8 radially is arranged on the outside of first interchanger 7 again.Shown in orthographic plan, first, second interchanger 7,8 and the 4 coaxial settings of first catalyst bed, therefore, the vertical central shaft of they and reaction vessel 1 is coaxial, and is located substantially on sustained height.
The flow direction of gas sees it is clearly from accompanying drawing separately in Fig. 3 and Fig. 4, they be described in this omission.
As top detailed as described in because catalyst bed and at least two heat exchangers of arranging with the vertical spigot shaft coaxle of reaction vessel, and they are located substantially on same vertical height, thereby have just formed especially some following advantages.
(1) heat exchanger is compared with other assembly in the catalytic reactor, and structure is complicated, but its special concentrated area is arranged on the catalytic reactor topmost portion, and the maintenance of heat exchanger here is easy, Thus, made things convenient for work such as the assembly and disassembly of heat exchanger.
(2) structure that the catalyst bed of interchanger is not set in catalyst bed can be simplified, so their maintenance is also convenient.
(3) simplify the one-piece construction of catalyticreactor, caused cost lower.
Claims (9)
1, a kind ofly gas raw material is contacted with solid catalyst make the generation exothermic shift reaction, thereby obtain the vertical catalyticreactor of gaseous reaction product, this reactor comprises: a reaction vessel, at least three catalyst beds in this reaction vessel, i.e. first catalyst bed, second catalyst bed and the 3rd catalyst bed, these catalyst beds are below one of the vertical central shaft of reaction vessel is arranged on another, and with the coaxial setting of vertical central shaft of reaction vessel, so that reactant gases is flow through there continuously; At least two interchanger in reactor, promptly corresponding to first interchanger of above-mentioned first catalytic bed with corresponding to second interchanger of above-mentioned second catalyst bed, the coaxial setting of vertical central shaft of these interchanger and reaction vessel, and be connected with catalyst bed respectively, so that from the reactant gases of each catalyst bed, before entering the next stage catalyst bed, in its corresponding interchanger, be cooled, each above-mentioned catalyst bed all be by can by gas and different diameter is arranged in, the out cylinder sidewall is formed, and with the coaxial setting of vertical central shaft of reaction vessel, upper end wall and lower end wall are located at respectively can be by in the gas, going up on terminal and the lower end of out cylinder sidewall, solid catalyst be seated in by can by gas in, out cylinder sidewall and last, in the annular space that lower end wall limited, thus, can make corresponding reactant gases radially flow through catalyst bed, it is characterized in that at least the first catalyst bed and at least two respectively corresponding to the interchanger of first catalyst bed and second catalyst bed, with the coaxial setting of the vertical central axis of reaction vessel and be positioned on the essentially identical height.
According to the catalyticreactor of claim 1, it is characterized in that 2, in each catalyst bed, reactant gases radially flows from the inside cylinder side wall of out cylinder sidewall.
3, according to the catalyticreactor of claim 1, it is characterized in that, in a catalyst bed, two interchanger are set at least radially at least.
4, according to the catalyticreactor of claim 1, it is characterized in that,, at least one interchanger in several interchanger is set radially respectively at the within and without of at least one described catalyst bed.
5, according to the catalyticreactor of claim 1, it is characterized in that,, at least two interchanger are set radially at least in the outside of a described catalyst bed.
According to the catalyticreactor of claim 1, it is characterized in that 6, at least one described catalyst bed is the catalyst bed of topmost in the catalyticreactor.
7, according to the anti-device of celebrating of the catalysis of claim 6, it is characterized in that, in a described catalyst bed, at least two interchanger are set radially at least.
According to the catalyticreactor of claim 6, it is characterized in that 8, at least one in several interchanger radially is arranged on the inside of at least one catalyst bed, and in several interchanger at least one radially is arranged on the outside of at least one this catalyst bed.
9, according to the catalyticreactor of claim 6, it is characterized in that,, two interchanger are set at least in the outside of at least one catalyst bed.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62118961A JPS63283741A (en) | 1987-05-18 | 1987-05-18 | Contact reaction device |
| JP118961/87 | 1987-05-18 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1030027A CN1030027A (en) | 1989-01-04 |
| CN1014118B true CN1014118B (en) | 1991-10-02 |
Family
ID=14749561
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN88102903.3A Expired CN1014118B (en) | 1987-05-18 | 1988-05-18 | Catalytic reactor |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US4942022A (en) |
| JP (1) | JPS63283741A (en) |
| CN (1) | CN1014118B (en) |
| DD (1) | DD269792A5 (en) |
| IN (1) | IN168953B (en) |
| MY (1) | MY103347A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101007256B (en) * | 2006-01-24 | 2012-02-29 | 百瑞全球有限公司 | Reactor |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3926105A1 (en) * | 1989-08-08 | 1991-02-14 | Metallgesellschaft Ag | DEVICE FOR CATALYTICALLY CONVERTING AN H (ARROW DOWN) 2 (ARROW DOWN) S AND SO (ARROW DOWN) 2 (ARROW DOWN) CONTAINING GAS MIXTURE |
| CN1039791C (en) * | 1993-12-24 | 1998-09-16 | 湖南省安淳节能技术有限公司 | Gas-solid catalyst reactor |
| IT1271798B (en) * | 1993-12-29 | 1997-06-09 | Ammonia Casale Sa | METHOD FOR THE MORDENIZATION IN SITU OF A REACTOR FOR EXOTHERMAL HETEROGENEOUS SYNTHESIS, IN PARTICULAR OF THE KELLOG TYPE |
| CA2415536A1 (en) * | 2002-12-31 | 2004-06-30 | Long Manufacturing Ltd. | Reformer for converting fuel to hydrogen |
| EP1442786A1 (en) * | 2003-01-29 | 2004-08-04 | Methanol Casale S.A. | Pseudo isothermal radial reactor |
| EP3037165A1 (en) * | 2014-12-23 | 2016-06-29 | Casale SA | Method for realizing internal walls of catalytic reactors |
| WO2024126824A1 (en) | 2022-12-16 | 2024-06-20 | Casale Sa | Methanol synthesis converter and process |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52141488A (en) * | 1976-05-21 | 1977-11-25 | Toyo Engineering Corp | Gassphase pressure contact reaction apparatus |
| US4372920A (en) * | 1979-07-13 | 1983-02-08 | Ammonia Casale S.A. | Axial-radial reactor for heterogeneous synthesis |
| US4637918A (en) * | 1983-03-07 | 1987-01-20 | Exxon Research & Engineering Co. | Catalytic gas synthesis apparatus |
| JPS60110328A (en) * | 1983-11-17 | 1985-06-15 | Toyo Eng Corp | Catalytic reactor |
| DE3343114C2 (en) * | 1983-11-29 | 1985-11-07 | Uhde Gmbh, 4600 Dortmund | Device for carrying out exothermic, catalytic gas reactions for ammonia or methanol synthesis |
| CH666198A5 (en) * | 1985-09-13 | 1988-07-15 | Ammonia Casale Sa | REACTOR FOR CATALYTIC SYNTHESIS OF AMMONIA, METHANOL AND HIGHER ALCOHOLS. |
-
1987
- 1987-05-18 JP JP62118961A patent/JPS63283741A/en active Pending
- 1987-08-24 IN IN665/CAL/87A patent/IN168953B/en unknown
- 1987-12-30 US US07/139,609 patent/US4942022A/en not_active Expired - Fee Related
-
1988
- 1988-01-07 MY MYPI88000011A patent/MY103347A/en unknown
- 1988-04-21 DD DD88314966A patent/DD269792A5/en not_active IP Right Cessation
- 1988-05-18 CN CN88102903.3A patent/CN1014118B/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101007256B (en) * | 2006-01-24 | 2012-02-29 | 百瑞全球有限公司 | Reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| DD269792A5 (en) | 1989-07-12 |
| JPS63283741A (en) | 1988-11-21 |
| MY103347A (en) | 1993-06-30 |
| US4942022A (en) | 1990-07-17 |
| IN168953B (en) | 1991-07-27 |
| CN1030027A (en) | 1989-01-04 |
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| C10 | Entry into substantive examination | ||
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| C13 | Decision | ||
| GR02 | Examined patent application | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |